Carbon dioxide purification

ABSTRACT

A process for the recovery of carbon dioxide from a gas mixture that includes pretreating a gas mixture comprising carbon dioxide, water vapor, and one or more light gases in a pretreating system to form a cooled gas mixture, fractionating the cooled gas mixture to recover a bottoms fraction comprising carbon dioxide and an overheads fraction comprising carbon dioxide and the light gases, passing the overheads fraction over a membrane selective to carbon dioxide to separate a carbon dioxide permeate from a residue gas comprising the light gases, recycling the carbon dioxide permeate to the pretreating system, and recovering at least a portion of the bottoms fraction as a purified carbon dioxide product stream is described.

BACKGROUND OF DISCLOSURE

1. Field of the Disclosure

Embodiments disclosed herein relate generally to a process for carbondioxide sequestration for producing a liquid carbon dioxide stream,which may be used, for example, for enhanced oil recovery. Morespecifically, embodiments disclosed herein relate to a process forcarbon dioxide purification integrating membrane technology, carbondioxide distillation, and use of carbon dioxide as a self-refrigerant toresult in an improved process capable of recovering a high percentage ofcarbon dioxide in the feed at a high purity.

2. Background

Various reservoir flooding techniques have been utilized by the oil andgas industry in enhanced oil recovery programs as a means to increasethe production of hydrocarbons. In carbon dioxide flooding, carbondioxide is pumped into the reservoir through an injection well forextended periods of time (e.g., years). The injected carbon dioxide“floods” the treated zone and forces/carries the oil in the formationtoward one or more production wells where the fluids are recovered. Thecomposition of the produced fluids changes with time and, at some point,carbon dioxide “breakthrough” will occur. After breakthrough the volumeof gas and the carbon dioxide content of the produced fluids increasesubstantially.

Carbon dioxide may represent 60-96 mol percent (or more) of the fluidsproduced. In order for carbon dioxide flooding operations to beeconomically viable, carbon dioxide must be efficiently recovered fromthe produced fluids for reuse. In many cases, recovered carbon dioxidecan be re-injected into the formation through the injection well,provided chemical specifications for purity are met. Productspecifications for carbon dioxide can be quite high, particularly withrespect to the content of hydrocarbons (i.e., methane and ethane) and/ornitrogen.

Carbon dioxide used in flooding operations may come from a variety ofsources, including off-gases from chemical processes, among othersources. Processes to purify such carbon dioxide-rich streams typicallyinvolve removal of light gases such as hydrogen, nitrogen, oxygen,methane, and carbon monoxide. Many of these streams have low carbondioxide content, including lime kiln gas, boiler flue gas and certainnatural gases.

To recover carbon dioxide from streams having a low carbon dioxidecontent, such as a boiler flue gas stream, one solution is to scrub thegas mixture which is lean in carbon dioxide with a suitable solvent,such as monoethanolamine, sulfolane or potassium carbonate, to dissolvethe carbon dioxide and then to strip the carbon dioxide from thesolution so obtained; i.e., another fluid is introduced into the systemin order to achieve the necessary separation. The carbon dioxide canthen be compressed, dried, cooled and further purified by partialcondensation or distillation. However this process is expensive inenergy and a less energy-intensive alternative would be desirable.

Various other processes to recover and/or purify carbon dioxide aredisclosed in U.S. Pat. Nos. 4,602,477, 4,639,257, 4,762,543, 4,936,887,6,070,431, and 7,124,605, among others.

Large scale carbon dioxide processes are also discussed in: Hegerland etal., “Liquefaction and handling of large amount of CO₂ for EOR,” ProjectInvest as, Norway, YARA International ASA (volume, date, etc.); Bergeret al, “Creating a large scale CO2 infrastructure for enhanced oilrecovery,” presented at the 7^(th) International Conference ofGreenhouse Gas Control Technologies, Vancouver, 2004; and in Song et al,SPE Formation Evaluation, Society of Petroleum Engineers, December 1987.

There remains a need for processes having improved carbon dioxiderecovery while maintaining a high purity for the recovered carbondioxide.

SUMMARY OF THE DISCLOSURE

In one aspect, embodiments disclosed herein relate to a process for therecovery of carbon dioxide from a gas mixture that includes pretreatinga gas mixture comprising carbon dioxide, water vapor, and one or morelight gases in a pretreating system to form a cooled gas mixture,fractionating the cooled gas mixture to recover a bottoms fractioncomprising carbon dioxide and an overheads fraction comprising carbondioxide and the light gases, passing the overheads fraction over amembrane selective to carbon dioxide to separate a carbon dioxidepermeate from a residue gas comprising the light gases, recycling thecarbon dioxide permeate to the pretreating system, and recovering atleast a portion of the bottoms fraction as a purified carbon dioxideproduct stream

Other aspects and advantages will be apparent from the followingdescription and the appended claims.

BRIEF DESCRIPTION OF DRAWINGS

FIG. 1 is a simplified flow diagram of a carbon dioxide purificationprocess according to embodiments disclosed herein.

FIG. 2 is a simplified flow diagram of a carbon dioxide purificationprocess according to embodiments disclosed herein.

FIG. 3 is a simplified flow diagram of a portion of a carbon dioxidepurification process according to embodiments disclosed herein.

DETAILED DESCRIPTION

In one aspect, embodiments herein relate to a process for carbon dioxidesequestration for producing a liquid carbon dioxide stream, which may beused, for example, for enhanced oil recovery. More specifically,embodiments disclosed herein relate to a process for carbon dioxidepurification integrating membrane technology, carbon dioxidedistillation, and use of carbon dioxide as a self-refrigerant to resultin an improved process capable of recovering a high percentage of carbondioxide in the feed at a high purity.

Processes disclosed herein may be useful for recovery and purificationof carbon dioxide from various sources, including boiler flue gas, limekiln gas, natural gases, and other off-gases from various processes. Insome embodiments, the stream from which carbon dioxide is to berecovered may contain at least 30%, by volume, carbon dioxide; at least40%, by volume, in other embodiments; at least 50%, by volume, in otherembodiments; at least 60%, by volume in other embodiments; and at least70%, by volume, in yet other embodiments. Such streams may also includeother light gases, including methane, oxygen, nitrogen, argon, and watervapor, for example. Even at low feed percentages, processes disclosedherein may recover a high percentage of the carbon dioxide contained inthe feed gas at a high carbon dioxide purity.

Referring now to FIG. 1, a simplified flow diagram of a carbon dioxidepurification process according to embodiments disclosed herein isillustrated. A stream containing carbon dioxide, other light gases, andwater vapor may be pretreated to compress and dry the gas mixture in apretreating system. As shown in FIG. 1, the pretreating system iscomprised of gas compression system 12, dryer 26 and compression system33. In other embodiments, other well known pretreatment systems can beused. For example, the gas mixture may be fed via flow line 10 to gascompression system 12. Gas compression system 12 may include one or morecompressors 14, coolers 16, and scrubbers 18. As illustrated, threecompression stages are included in gas compression system 12. The actualnumber of stages used may depend on the desired pressure increase, powerdistribution, discharge temperatures, and polytropic compressorefficiencies, among other variables.

After each stage of compression, the gas exiting compressors 14 may becooled by coolers 16. For example, the gas may be cooled to atemperature in the range from about 15° C. to about 40° C., such asabout 30° C., where the resulting temperature may depend upon the typeof cooler, temperature of a heat exchange medium, or ambienttemperature, among other factors. In some embodiments, coolers 16 mayinclude air coolers.

Following each stage of compression and cooling, condensed water may beremoved from the gas in scrubbers 18. Scrubbers 18 may be equipped, forexample, with mist eliminators or other devices to separate entrainedwater droplets from the gas stream. The water may be recovered fromscrubbers 18 via outlets 20, and in some embodiments may be drained to awastewater treatment system (not shown).

Following compression system 12, the resulting compressed gas stream maybe recovered via flow line 22. Additional water may be removed from thecompressed gas in flow line 22 by passing the gas over a solid desiccant24 contained in a dryer 26. Desiccant 24 may include, for example, type3A molecular sieves, among other desiccants known in the art.

A dried compressed gas stream may be recovered from dryer 26 via flowline 28. In some embodiments, the compressed gas recovered from dryer 26may have less than 200 ppm water, by volume; less than 100 ppm, byvolume, in other embodiments, and less than 50 ppm, by volume, in yetother embodiments. Removal of water may attenuate the occurrences ofcorrosion in downstream processing equipment and water freezing duringthe processing and transportation of the product carbon dioxide. A dustfilter 30 may be provided at the outlet of dryer 26 to remove any finesthat the gas stream may pick up from desiccant 24.

Dried gas stream 32 may then be compressed via compression system 33,including one or more compressors 34 and one or more coolers 36, toresult in a compressed gas stream 38 having the desired inlet gaspressure for purification system 40. In some embodiments, compressed gasstream 38 may have a pressure of at least 40 bar; compressed gas stream38 may have a pressure in the range from about 40 to about 60 bar inother embodiments; from about 43 to about 55 bar in other embodiments;and from about 46 to about 52 bar, such as about 49 bar, in yet otherembodiments.

Following pretreatment, compressed gas stream 38 may then be chilled viaone or more heat exchangers 88 and fed to column 44 via flow line 46.The gas feed to column 44 may be cooled to a temperature in the rangefrom about −30° C. to about −35° C., such as about −33° C., for example.

Column 44 may include a series of trays or packed beds above and/orbelow the feed inlet location to facilitate fractionation of the carbondioxide, recovered as a bottoms fraction via flow line 48, from theoverhead gas fraction, recovered via flow line 50. In order to refluxthe trays or packed beds in upper section 52 of column 44, a portion ofthe overhead fraction recovered via flow line 50 may be condensed, viaremoval of heat in one or more heat exchangers 53, accumulated in drum54, and recycled via flow line 56 as reflux. To effect the condensationof vapors, the overheads fraction may be cooled to a temperature in therange from about −50° C. to about −65° C. in some embodiments; and fromabout −55 to about −60° C., such as about −57° C., in other embodiments.

The carbon dioxide bottoms stream 48 may be fed to a surge tank 60. Aportion of the recovered bottoms fraction may be heated via reboiler 62and fed to column 44 to control the vapor traffic within the column. Theremaining portion of the recovered bottoms fraction may be recovered asa carbon dioxide product stream via flow line 64. In some embodiments,the carbon dioxide product stream recovered may have be at least 90%carbon dioxide, by volume; at least 95% by volume in other embodiments;at least 97% by volume in other embodiments; at least 98% by volume inother embodiments; and at least 99% by volume in yet other embodiments.

The vapor fraction recovered from drum 54 via flow line 58 may include amajority of the light gases contained in the initial feed stream 10 aswell as carbon dioxide. Additional carbon dioxide may be recovered bypassing the vapor fraction in flow line 58 through a membrane unit 66. Acompressor may be added in front of the membrane unit 66 to allow thecolumn 44 to operate at a lower pressure and the membrane to operate ata higher pressure. Membrane unit 66 separates additional carbon dioxidefrom the other light gases by diffusion when the vapor fraction ispassed across a membrane selective for carbon dioxide, where thediffusion rate may be a function of the area of the membranes used andthe differential concentration of carbon dioxide across the one or moremembranes. The carbon dioxide permeate, having passed through themembrane, may be recovered via flow line 68 and recycled to compressionsystem 12. As illustrated, the carbon dioxide permeate is recycled tothe second compression stage, however, the carbon dioxide permeate canrecycled to any point of gas compression system 12. The residue, havingdecreased carbon dioxide content, may be recovered via flow line 70.

In some embodiments, at least 50%, by volume, of the carbon dioxide fedto membrane unit 66 may be recovered via flow line 68; at least 60%, byvolume, in other embodiments; and at least 70%, by volume, in yet otherembodiments.

The carbon dioxide purification according to embodiments describedherein may allow for a high purity carbon dioxide stream 64 to berecovered, as described above. The additional carbon dioxide recoveredvia membrane unit 66 may allow the overall carbon dioxide purificationprocess to recover greater than 65 mole %, of the carbon dioxide presentin feed stream 10; a recovery of greater than 75 mole % may be achievedin other embodiments; a recovery of greater than 90 mole % may beachieved in other embodiments; greater than 95 mole % in yet otherembodiments. In select embodiments, greater than 90 mole % of the carbondioxide may be recovered at a purity of at least 95%, by volume.

In addition to the improved separations that may be attained byprocesses according to embodiments disclosed herein, it has also beenfound that additional efficiencies may be realized by using the variouscarbon dioxide streams as a self-refrigerant, an example of which isillustrated in FIG. 2, where like numerals represent like parts.

The compressed gas stream 38 may be used as a hot side fluid in reboiler62 in some embodiments, producing reboil vapor and cooling thecompressed gas following compression system 33. The resulting cooledcompressed gas stream 72 may then be split into two or more fractionsand cooled, using one or more of a portion of the carbon dioxide productstream 64, vapor fraction 58 recovered from drum 54, and a refrigerant,prior to feeding the compressed gas to column 44 via flow line 46.

As illustrated in FIG. 2, compressed gas stream 72 may be split intothree fractions, including flow streams 74, 76, and 78. Fraction 74 maybe cooled via indirect heat exchange with a portion of the carbondioxide product 64 in heat exchanger 80 via flow lines 84 and 86. Theslip stream of carbon dioxide product may then be fed via flow line 82to compression system 12, such as to the third stage compressor.

In some embodiments, as illustrated, a portion of the carbon dioxideproduct stream 64 may be fed via flow line 84 and used to condense aportion of the overheads fraction from flow line 50 in heat exchanger53. The slip stream of carbon dioxide vaporized or boiled from the coldside of heat exchanger 53 may then be fed via flow line 86 to coolfraction 74 in heat exchanger 80.

Fraction 76 may be cooled via indirect heat exchange with vapor fraction58 recovered from drum 54 in heat exchanger 87. Optionally, a compressor59 may be added in front of the membrane unit 66 to allow the column 44to operate at a lower pressure and the membrane unit 66 to operate at ahigher pressure.

Fraction 78 may be cooled via indirect heat exchange with a refrigerantin heat exchanger 88. The three fractions 74, 76, 78 may then berecombined via flow lines 90, 92, 94 and fed via flow line 46 to column44. The amount of feed gas fed through each of lines 74, 76, 78 maydepend upon the heat exchange requirements, including the temperature ofcompressed gas streams 38, 72, the desired feed temperature, and thetemperatures of streams 58, 64, 86, and the refrigerant, among othervariables.

In some embodiments, the refrigerant used for indirect heat exchange inheat exchanger 88 is propane; other refrigerants or mixtures ofrefrigerants may also be used. The propane may be circulated inrefrigeration loop 96, which may include compressors 98, which mayinclude two-stage compression systems, cooler 100, accumulator 102, andeconomizer 104. The vapor from economizer 104 may be recycled to thesuction of the second stage compressor, and the liquid may be fed toheat exchanger 88, cooling the compressed feed 78 to a temperature belowabout −33° C., such as to a temperature within the range from about −25°C. to about −40° C. Flashed propane from heat exchanger 88 may be fedvia flow line 106 to scrubber 108 and then to compressor 98.

Additional efficiencies may also be realized by recovery and reuse ofresidue stream 70 recovered from membrane 66, an example of which isillustrated in FIG. 3, where like numerals represent like parts. Aportion of residue stream 70 may be heated to an elevated temperature,such as a temperature greater than 200° C. in some embodiments, inheater 110, such as an electric heater. The heated residue gas may thenbe fed via flow line 112 to the dryer 26 (26 a or 26 b) beingregenerated to remove water adsorbed by the desiccant. In thisembodiment, the carbon dioxide purification system includes at least twodryers 26 a, 26 b, where one bed of desiccant, such as bed 24 a, may bein use while the other bed of desiccant, such as bed 24 b, is beingregenerated (valve positioning not illustrated). The regeneration gasmay then be recovered via flow line 114, and optionally cooled torecover water using cooler 116 and scrubber 118. The gas used toregenerate the beds and any unused portion of residue gas 70 may then becombined in flow stream 120 for further recovery, treatment, ordisposal.

As described above, embodiments of the carbon dioxide purificationsystem advantageously provide for the recovery of 90% or more of thecarbon dioxide in the feed at a purity of 95% or more. Advantageously,processes disclosed herein may be used to recover high purity carbondioxide streams from low carbon dioxide content streams, includingboiler flue gas and lime kiln gas, among others, without the use ofsolvents, such as amines. The purified carbon dioxide decreases theamount of carbon dioxide contributing to the greenhouse gas inventory ofa production facility, and may be used for enhanced oil recovery, or maybe her purified for use in carbonated drinks. Embodiments disclosedherein also provide for the advantageous use of waste gas streams andproduct streams for heat recovery, and desiccant regeneration.

While the disclosure includes a limited number of embodiments, thoseskilled in the art, having benefit of this disclosure, will appreciatethat other embodiments may be devised which do not depart from the scopeof the present disclosure. Accordingly, the scope should be limited onlyby the attached claims.

1. A process for the recovery of carbon dioxide from a gas mixture, theprocess comprising: pretreating a gas mixture comprising carbon dioxide,water vapor, and one or more light gases in a pretreating system to forma cooled gas mixture; fractionating the cooled gas mixture to recover abottoms fraction comprising carbon dioxide and an overheads fractioncomprising carbon dioxide and the light gases; passing the overheadsfraction over a membrane selective to carbon dioxide to separate acarbon dioxide permeate from a residue gas comprising the light gases;recycling the carbon dioxide permeate to the pretreating system; andrecovering at least a portion of the bottoms fraction as a purifiedcarbon dioxide product stream.
 2. The process of claim 1, wherein thepretreating comprises compressing the gas mixture.
 3. The process ofclaim 2, wherein the pretreating further comprises drying the compressedgas mixture.
 4. The process of claim 3, wherein the drying comprises atleast one of contacting the gaseous mixture with a desiccant andseparating condensed water from the compressed gas mixture.
 5. Theprocess of claim 3, further comprising using at least a portion of theresidue gas to regenerate a desiccant used in the drying.
 6. The processof claim 1, wherein the pretreated gas comprises less than 50 ppm water,by volume.
 7. The process of claim 1, wherein the fractionating isperformed at a pressure in the range from about 40 to about 60 bar. 8.The process of claim 1, further comprising cooling the pretreated gasmixture to condense at least a portion of the carbon dioxide.
 9. Theprocess of claim 8, wherein the cooling the pretreated gas mixturecomprises indirect heat exchange of the pretreated gas mixture with atleast one of a refrigerant, at least a portion of the bottoms fraction,and at least a portion of the overheads fraction.
 10. The process ofclaim 9, wherein the refrigerant comprises propane.
 11. The process ofclaim 9, wherein the cooling decreases the pretreated gas to atemperature in the range from about −30° C. to about −35° C.
 12. Theprocess of claim 1, wherein the carbon dioxide product stream comprisesat least 95%, by volume, carbon dioxide.
 13. The process of claim 12,wherein at least 90% of the carbon dioxide in the gas mixture isrecovered in the carbon dioxide product stream.
 14. A process for therecovery of carbon dioxide from a gas mixture, the process comprising:pretreating a gas mixture comprising carbon dioxide, water vapor, andone or more light gases in a pretreating system to form a cooled gasmixture; fractionating the cooled gas mixture to recover a bottomsfraction comprising carbon dioxide and an overheads fraction comprisingcarbon dioxide and the light gases; contacting at least a portion of thebottoms fraction via indirect heat exchange with the overheads fractionto form an overheads vapor fraction and an overheads liquid fraction;passing the overheads vapor fraction over a membrane selective to carbondioxide to separate a carbon dioxide permeate from a residue gascomprising the light gases; recycling the carbon dioxide permeate andthe at least a portion of the bottoms fraction to the pretreatingsystem; and recovering at least a portion of the bottoms fraction as apurified carbon dioxide product stream.
 15. The process of claim 14,further comprising feeding the overheads liquid fraction as reflux forthe fractionating.
 16. The process of claim 14, wherein the pretreatingcomprises compressing and drying the gas mixture.
 17. The process ofclaim 16, further comprising using at least a portion of the residue gasto regenerate a desiccant used in the drying.
 18. The process of claim14, further comprising condensing at least a portion of the carbondioxide in the pretreated gas via indirect heat exchange with at leastone of: at least a portion of the bottoms fraction; at least a portionof the overheads vapor fraction; and a refrigerant.
 19. The process ofclaim 18, further comprising returning the at least a portion of thebottoms fraction recovered from indirect heat exchange with thepretreated gas to the column as reboil vapor.
 20. The process of claim18, further comprising contacting at least a portion of the pretreatedgas via indirect heat exchange with the at least a portion of thebottoms fraction recovered from the indirect heat exchange with theoverheads fraction.
 21. The process of claim 14, wherein the carbondioxide product stream comprises at least 95%, by volume, carbondioxide.
 22. The process of claim 21, wherein at least 90% of the carbondioxide in the gas mixture is recovered in the carbon dioxide productstream.
 23. A process for the recovery of carbon dioxide from a gasmixture, the process comprising: pretreating a gas mixture comprisingcarbon dioxide, water vapor, and one or more light gases in apretreating system to form a cooled gas mixture; separating said cooledgas mixture into at least a first stream, a second stream, and a thirdstream; contacting at least a portion of said first stream via indirectheat exchange with a refrigerant; contacting at least a portion of saidsecond stream via indirect heat exchange with an overheads vaporfraction from a fractionator to form a cooled overheads vapor fraction;passing said cooled overheads vapor fraction over a membrane selectiveto carbon dioxide to separate a carbon dioxide permeate from a residuegas comprising the light gases; recycling at least a portion of thecarbon dioxide permeate to the pretreating system; contacting at least aportion of said third stream via indirect heat exchange with at least aportion of a bottoms fraction from a fractionator to form a cooledbottoms fraction; recycling at least a portion of said cooled bottomsfraction to said pretreating system; recombining said first, second, andthird streams to form a recombined stream; fractionating said recombinedstream to form said bottoms fraction stream comprising carbon dioxideand an overheads fraction comprising carbon dioxide and the light gases;contacting at least a portion of the bottoms fraction via indirect heatexchange with the overheads fraction to form said overheads vaporfraction and an overheads liquid fraction; and recovering at least aportion of the bottoms fraction as a purified carbon dioxide productstream.